JP5513980B2 - Absorption heat pump - Google Patents

Description

  The present invention relates to an absorption heat pump, and more particularly, to an absorption heat pump that can be operated with an appropriate COP while allowing an increase in heating capability.

  In the type 2 absorption heat pump, which is a temperature rising type heat pump that takes out a heated medium having a temperature higher than the driving heat source temperature, the temperature of the heated medium is increased because the heated medium is taken out as high-temperature water or high-temperature steam having high utility value. In order to increase the width, there is a multistage temperature rising type absorption heat pump in which absorbers are configured in multiple stages. As an example of a multi-stage temperature rising type absorption heat pump, a common evaporator is used to generate refrigerant vapor to be supplied to the high temperature side absorber and the low temperature side absorber, and the operating pressures of the high temperature side absorber and the low temperature side absorber are made equal. A two-stage temperature rising absorption heat pump (for example, refer to Patent Document 1) that suppresses an increase in internal pressure, a high temperature side evaporator that generates refrigerant vapor to be supplied to the high temperature side absorber, and a refrigerant to be supplied to the low temperature side absorber. A two-stage temperature rise type that separately installs a low-temperature side evaporator that generates steam and operates the high-temperature side absorber at a higher pressure than the low-temperature side absorber to suppress the concentration rise near the crystal line of the absorbent There exists an absorption heat pump (for example, refer patent document 2).

JP 59-115952 (FIG. 2 etc.) JP 2006-112686 A (FIG. 6 etc.)

  However, in the two-stage temperature rising type absorption heat pump described in Patent Document 1 and Patent Document 2, the range in which the medium to be heated can be raised is limited, and the temperature raising ability may be insufficient. In order to improve the temperature raising capability, it is conceivable to configure the absorber in multiple stages. However, as the number of absorbers is increased, not only the problem of internal pressure or crystals occurs, but also the COP (coefficient of performance) decreases. There was a problem that.

  In view of the above-described problems, an object of the present invention is to provide an absorption heat pump that can be operated with an appropriate COP while enabling an increase in heating capability.

  In order to achieve the above object, the absorption heat pump according to the first aspect of the present invention has a flow path 11 of the medium to be heated W inside, for example, as shown in FIG. A first absorber 10 that heats the medium W to be heated with absorption heat generated when absorbing the first refrigerant vapor Vr; and an evaporator 20 that supplies the first refrigerant vapor Vr to the first absorber 10. And the second absorbing liquid Sb heats the refrigerant liquid Vf in the evaporator 20 with the absorption heat generated when the second refrigerant vapor Vs absorbs the second refrigerant vapor Vs, thereby generating the first refrigerant vapor Vr. A second absorber 30 having an operating temperature lower than that of the absorber 10; and the first absorbent 10 in the first absorber 10 absorbs the first refrigerant vapor Vr and directly reduces the diluted solution Sw. The second absorbent Sb absorbs the second refrigerant vapor Vs in the second absorber 30. The first regenerator 60 that introduces the diluted solution Sv having a reduced concentration and heats it to evaporate the refrigerant from the diluted solution Sx (Sw, Sv) to generate the intermediate concentration absorbing solution Sb having an increased concentration. A second regenerator 50 that introduces and heats the intermediate concentration absorbing liquid Sb from the first regenerator 60 and generates the first absorbing liquid Sa; and the absorption heat generated in the second absorber 30 directly Absorption heat transfer means 51 for transferring the heat into the second regenerator 50 intentionally or indirectly. Here, the first regenerator 60 directly introduces the dilute solution Sw whose concentration is lowered by the first absorber 10 absorbing the first refrigerant vapor Vr in the first absorber 10. Is typically introduced without passing through the second absorber 30, and indirectly introduced is typically introduced through the second absorber 30.

  If comprised in this way, both the dilute solution derived | led-out from the 1st absorber and the dilute solution derived | led-out from the 2nd absorber are directly or indirectly introduce | transduced into a 1st regenerator, and intermediate concentration absorption is carried out. The intermediate concentration absorbing liquid is regenerated in the second regenerator after being made into a liquid, and the heat input to the first regenerator is utilized to the maximum as the heat used for regenerating the solution. Thus, COP can be improved.

  Moreover, the absorption heat pump according to the second aspect of the present invention is, for example, as shown in FIG. 1, in the absorption heat pump 1 according to the first aspect of the present invention, the absorption heat transfer means is the first in the evaporator 20. 1 is a refrigerant vapor heat source pipe 51 for flowing one refrigerant vapor Vr therein, and is constituted by a refrigerant vapor heat source pipe 51 disposed so as to pass through the second regenerator 50; A refrigerant vapor heat source flow rate adjustment valve 51v for adjusting the flow rate of the flowing first refrigerant vapor is further provided.

  With this configuration, the amount of heat input to the second regenerator can be adjusted, and it is possible to avoid crystals of the absorbing liquid in the second regenerator.

  Moreover, the absorption heat pump according to the third aspect of the present invention is, for example, as shown in FIG. 4, in the absorption heat pump 2 according to the first aspect of the present invention, the absorption heat transfer means includes the heat medium t inside. A heat medium pipe 251 that is sealed to flow, and is configured to pass through the second absorber 30 and the second regenerator 50; heat in the heat medium pipe 251; A heat medium fluidizing device 259 for causing the medium t to flow, the heat medium fluidizing device 259 configured to be able to change the flow rate of the heat medium t.

  With this configuration, the amount of heat input to the second regenerator can be adjusted, and it is possible to avoid crystals of the absorbing liquid in the second regenerator.

  Moreover, the absorption heat pump according to the fourth aspect of the present invention is the absorption heat pump according to any one of the first to third aspects of the present invention, as shown in FIG. Among the second absorbing liquid Sb (Sw) introduced into the absorber 30, the absorbing liquid flow rate adjusting means 35 for adjusting the flow rate of the second absorbing liquid Sb (Sw) that absorbs the second refrigerant vapor Vs, 35v.

  With this configuration, it is possible to adjust the amount of heat absorbed by the second absorber related to the generation amount of the first refrigerant vapor, and thus adjust the amount of heat input to the second regenerator. This makes it possible to avoid the absorption liquid crystal in the second regenerator.

  According to the present invention, both the dilute solution derived from the first absorber and the dilute solution derived from the second absorber are directly or indirectly introduced into the first regenerator to absorb the intermediate concentration. The intermediate concentration absorbing liquid is regenerated in the second regenerator after being made into a liquid, and the heat input to the first regenerator is utilized to the maximum as the heat used for regenerating the solution. Thus, COP can be improved.

1 is a schematic system diagram of an absorption heat pump according to a first embodiment of the present invention. It is a Duhring diagram of the absorption heat pump concerning a 1st embodiment of the present invention. It is a Duhring diagram of the three-step temperature rising type absorption heat pump which concerns on a reference example. (A) shows a series flow, and (b) shows a parallel flow. It is a figure explaining the absorption heat pump which concerns on the 2nd Embodiment of this invention. (A) is a schematic systematic diagram, and (b) is a dueling diagram. It is a partial systematic diagram around the low-temperature absorber of the absorption heat pump which concerns on embodiment of this invention.

  Embodiments of the present invention will be described below with reference to the drawings. In the drawings, the same or similar members are denoted by the same or similar reference numerals, and redundant description is omitted.

  First, an absorption heat pump 1 according to a first embodiment of the present invention will be described with reference to FIG. FIG. 1 is a schematic system diagram of the absorption heat pump 1. The absorption heat pump 1 is a three-stage temperature rising type absorption heat pump that raises the temperature in the concentration direction and the pressure direction, respectively. The absorption heat pump 1 is a first component that heats the heated medium W with heat absorbed when the high-temperature concentrated solution Sa as the first absorption liquid absorbs the high-temperature refrigerant vapor Vr as the first refrigerant vapor. A high-temperature absorber 10 as an absorber, a high-temperature evaporator 20 as an evaporator for supplying the high-temperature refrigerant vapor Vr to the high-temperature absorber 10, and a second absorber having a lower operating temperature than the high-temperature absorber 10. The low temperature absorber 30, the low temperature evaporator 40 that supplies the low temperature refrigerant vapor Vs as the second refrigerant vapor to the low temperature absorber 30, and the dilute solution in which the high temperature concentrated solution Sa absorbs the high temperature refrigerant vapor Vr and the concentration is reduced. In the low-temperature absorber 30 and the low-temperature concentrated solution Sb as the second absorbent in the low-temperature absorber 30, the low-temperature diluted solution Sv as a diluted solution that has absorbed the low-temperature refrigerant vapor Vs and reduced in concentration is heated. With absorption liquid A low-temperature regenerator 60 as a first regenerator for generating a low-temperature concentrated solution Sb, a high-temperature regenerator 50 as a second regenerator for regenerating the low-temperature concentrated solution Sb into a high-temperature concentrated solution Sa, and a high-temperature regenerator A regenerator refrigerant vapor Vg in which the refrigerant evaporated from the low temperature concentrated solution Sb and the refrigerant evaporated from the dilute solution Sw and Sv in the low temperature regenerator 60 is cooled and condensed is provided.

  Further, the absorption heat pump 1 introduces a refrigerant vapor heat source pipe 51 as absorption heat transfer means disposed so as to pass through the inside of the high-temperature regenerator 50 and the heated medium W heated by the high-temperature absorber 10. A gas-liquid separator 80 that separates a heated medium vapor Wv, which is a gaseous heated medium W, and a heated medium liquid Wq, which is a liquid heated medium W, and a control device 99. In the present embodiment, the absorption heat pump 1 supplies the low-temperature regenerator 60 and the low-temperature evaporator 40 with the low-temperature (for example, about 80 ° C. to 90 ° C.) waste water h having a relatively low utility value as a heat source medium. High-value steam Wv (for example, the pressure exceeds about 0.2 MPa (gauge pressure), desirably about 0.8 MPa (gauge pressure)) can be taken out from the gas-liquid separator 80.

In the following description, in order to facilitate the distinction on the heat pump cycle with respect to the absorbing liquid, “high temperature dilute solution Sw”, “low temperature dilute solution Sv”, “high temperature dilute” depending on properties and positions on the heat pump cycle. Although they are referred to as “concentrated solution Sa”, “low temperature concentrated solution Sb”, etc., they are collectively referred to as “absorbing liquid S” when the properties are not questioned. Similarly, regarding the refrigerant, in order to facilitate the distinction on the heat pump cycle, “high temperature refrigerant vapor Vr”, “low temperature refrigerant vapor Vs”, “regenerator refrigerant vapor Vg”, depending on properties and positions on the heat pump cycle, Although it is referred to as “refrigerant liquid Vf” or the like, it is generally referred to as “refrigerant V” when the property or the like is not questioned. In the present embodiment, an LiBr aqueous solution is used as the absorbing liquid S (a mixture of the absorbent and the refrigerant V), and water (H ₂ O) is used as the refrigerant V. The heated medium W is a heated medium liquid Wq which is a liquid heated medium W, a heated medium vapor Wv which is a gaseous heated medium, and the heated medium liquid Wq and the heated medium vapor Wv are mixed. A general term for the mixed medium Wm to be heated. In the present embodiment, water (H ₂ O) is used as the heating medium W.

  The high-temperature absorber 10 includes a heating tube 11 that forms a flow path of the medium to be heated W and a high-temperature concentrated solution spray nozzle 12 that sprays the high-temperature concentrated solution Sa. The hot concentrated solution spray nozzle 12 is disposed above the heating tube 11 so that the sprayed hot concentrated solution Sa falls on the heating tube 11. The high temperature absorber 10 sprays the high temperature concentrated solution Sa from the high temperature concentrated solution spray nozzle 12 and generates heat of absorption when the high temperature concentrated solution Sa absorbs the high temperature refrigerant vapor Vr. The heated medium W flowing through the heating tube 11 receives this absorbed heat so that the heated medium W is heated. In the lower part of the high-temperature absorber 10, a storage part 13 is formed in which the high-temperature dilute solution Sw that has been dispersed by the dispersed high-temperature concentrated solution Sa absorbing the high-temperature refrigerant vapor Vr is stored. The heating tube 11 is disposed above the storage unit 13 so as not to be immersed in the hot dilute solution Sw. If it does in this way, generated absorbed heat will be quickly transmitted to the to-be-heated medium W which flows through the heating pipe | tube 11, and recovery | restoration of absorption capability can be accelerated. The storage unit 13 is provided with a high-temperature absorber liquid level detector 14 for detecting the liquid level of the stored high-temperature dilute solution Sw, and a high temperature for deriving the high-temperature dilute solution Sw toward the low-temperature regenerator 60. One end of the dilute solution tube 16 is connected.

  The high temperature evaporator 20 is a component that supplies the high temperature refrigerant vapor Vr to the high temperature absorber 10. The high-temperature evaporator 20 includes a refrigerant gas-liquid separation cylinder 21 that stores the refrigerant liquid Vf and the high-temperature refrigerant vapor Vr, a refrigerant liquid supply pipe 22 that guides the refrigerant liquid Vf to the heating pipe 31 of the low-temperature absorber 30, and the heating pipe 31. A high-temperature refrigerant vapor receiving pipe 24 that guides the high-temperature refrigerant vapor Vr generated by heating the refrigerant liquid Vf or a refrigerant gas-liquid mixed phase of the high-temperature refrigerant vapor Vr and the refrigerant liquid Vf to the refrigerant gas-liquid separation cylinder 21; A baffle plate 25 that collides and separates the droplets of the refrigerant V contained in the high-temperature refrigerant vapor Vr in the separation cylinder 21, and a high-temperature evaporator liquid level that detects the liquid level of the refrigerant liquid Vf in the refrigerant gas-liquid separation cylinder 21. The inner surface of the heating tube 31 is used as the heat transfer surface of the high-temperature evaporator 20. The high-temperature evaporator 20 is connected to a refrigerant liquid pipe 29 for introducing the refrigerant liquid Vf. One end of the refrigerant liquid supply pipe 22 is connected to the portion of the refrigerant gas-liquid separation cylinder 21 where the refrigerant liquid Vf is stored, and the other end is connected to one end of the heating pipe 31. The high-temperature refrigerant vapor receiving pipe 24 is disposed so that one end is located at a height between the highest liquid level of the refrigerant liquid Vf in the refrigerant gas-liquid separation cylinder 21 and the baffle plate 25, and the other end is the heating pipe 31. Is connected to the other end. The high-temperature evaporator liquid level detector 26 is connected to a two-way valve 29v disposed in the refrigerant liquid pipe 29 by a signal cable, and the refrigerant gas-liquid separation cylinder 21 is provided in accordance with the detected liquid level of the refrigerant liquid Vf. It is comprised so that the flow volume of the refrigerant | coolant liquid Vf introduce | transduced into can be adjusted. Since the refrigerant liquid Vf changes to steam inside the heating pipe 31 and the density is significantly reduced, the refrigerant liquid Vf is pumped in the refrigerant liquid supply pipe 22 by causing the heating pipe 31 to function as a bubble pump. The pump can be omitted. A pump for pumping the refrigerant liquid Vf may be provided in the refrigerant liquid supply pipe 22, and in this case, the heat transfer is improved by optimizing the flow rate in the pipe (optimizing the degree of the two-phase flow in the pipe). It is also possible.

  The high temperature absorber 10 and the high temperature evaporator 20 are formed in one can body so as to communicate with each other. The high temperature absorber 10 and the high temperature evaporator 20 communicate with each other so that the high temperature refrigerant vapor Vr in the high temperature evaporator 20 can be supplied to the high temperature absorber 10. The high-temperature absorber 10 and the high-temperature evaporator 20 typically communicate with each other above the high-temperature concentrated solution spray nozzle 12 and above the baffle plate 25.

  The low-temperature absorber 30 includes a heating pipe 31 that forms a flow path for the refrigerant liquid Vf and the high-temperature refrigerant vapor Vr, and a low-temperature concentrated solution spray nozzle 32 that sprays the low-temperature concentrated solution Sb. As described above, the heating pipe 31 has one end connected to the refrigerant liquid supply pipe 22 and the other end connected to the high-temperature refrigerant vapor receiving pipe 24. The low temperature concentrated solution spray nozzle 32 is disposed above the heating tube 31 so that the sprayed low temperature concentrated solution Sb falls on the heating tube 31. One end of a low-temperature concentrated solution tube 38 that allows the low-temperature concentrated solution Sb to flow inside is connected to the low-temperature concentrated solution spray nozzle 32. The low-temperature absorber 30 sprays the low-temperature concentrated solution Sb from the low-temperature concentrated solution spray nozzle 32, and heats the refrigerant liquid Vf flowing through the heating pipe 31 by heat absorbed when the low-temperature concentrated solution Sb absorbs the low-temperature refrigerant vapor Vs. Thus, the high-temperature refrigerant vapor Vr can be generated. The low temperature absorber 30 is configured to operate at a pressure (dew point temperature) lower than that of the high temperature absorber 10, and the operating temperature is lower than that of the high temperature absorber 10. In the lower part of the low-temperature absorber 30, a storage part 33 is formed in which the sprayed low-temperature concentrated solution Sb absorbs the low-temperature refrigerant vapor Vs to store the low-temperature dilute solution Sv having a reduced concentration. The heating tube 31 is disposed above the storage unit 33. The storage unit 33 is provided with a low-temperature absorber liquid level detector 34 for detecting the liquid level of the stored low-temperature dilute solution Sv, and a low temperature for deriving the low-temperature dilute solution Sv toward the low-temperature regenerator 60. One end of the dilute solution pipe 36 is connected.

  The low-temperature evaporator 40 includes a heat source pipe 41 as a first heat source medium pipe that constitutes a flow path of the exhaust hot water h as a heat source medium, and a refrigerant liquid spray nozzle 42 that sprays the refrigerant liquid Vf. Yes. The refrigerant liquid spray nozzle 42 is disposed above the heat source pipe 41 so that the sprayed refrigerant liquid Vf falls on the heat source pipe 41. One end of a refrigerant liquid pipe 48 through which the refrigerant liquid Vf flows is connected to the refrigerant liquid spray nozzle 42. The refrigerant liquid pipe 48 is provided with a flow rate adjusting valve 48v for adjusting the flow rate of the refrigerant liquid Vf supplied to the refrigerant liquid spraying nozzle 42. In the low-temperature evaporator 40, the refrigerant liquid Vf is sprayed from the refrigerant liquid spray nozzle 42, and the sprayed refrigerant liquid Vf is evaporated by the heat of the exhausted hot water h flowing in the heat source pipe 41 to generate the low-temperature refrigerant vapor Vs. It is configured. The low temperature evaporator 40 is configured to operate at a pressure (dew point temperature) lower than that of the high temperature evaporator 20, and the operating temperature is lower than that of the high temperature evaporator 20. In the lower part of the low-temperature evaporator 40, a storage part 43 is formed in which the refrigerant liquid Vf that has not evaporated out of the refrigerant liquid Vf introduced and dispersed from the condenser 70 is stored. A refrigerant liquid pipe 45 that guides the stored refrigerant liquid Vf to the condenser 70 is connected to the storage unit 43. The heat source tube 41 is disposed above the storage unit 43. The storage unit 43 is provided with a low-temperature evaporator liquid level detector 44 that detects the liquid level of the stored refrigerant liquid Vf. The low-temperature evaporator liquid level detector 44 is connected to the flow rate adjusting valve 48v disposed in the refrigerant liquid pipe 48 by a signal cable, and is introduced into the low-temperature evaporator 40 according to the detected liquid level of the refrigerant liquid Vf. The flow rate of the refrigerant liquid Vf can be adjusted.

  The low temperature absorber 30 and the low temperature evaporator 40 are formed in one can body so as to communicate with each other. The low temperature absorber 30 and the low temperature evaporator 40 communicate with each other so that the low temperature refrigerant vapor Vs generated in the low temperature evaporator 40 can be supplied to the low temperature absorber 30. The low-temperature absorber 30 and the low-temperature evaporator 40 typically communicate with each other above the low-temperature concentrated solution spray nozzle 32 and above the refrigerant liquid spray nozzle 42.

  The low-temperature regenerator 60 sprays a mixed source solution Sx in which a low-temperature dilute solution Sv and a high-temperature dilute solution Sw are mixed, and a heat source tube 61 as a second heat source medium tube that constitutes a flow path of exhaust hot water h as a heat source medium. And a mixed dilute solution spraying nozzle 62. In the present embodiment, the exhaust warm water h flowing through the heat source pipe 41 of the low temperature evaporator 40 and the exhaust warm water h flowing through the heat source pipe 61 of the low temperature regenerator 60 are the same hot water, and the exhaust warm water h flowing through the heat source pipe 41 is the same. Are connected by piping (not shown) so as to flow through the heat source pipe 61 thereafter, but different heat source media may flow through the heat source pipes 41 and 61. The mixed dilute solution spray nozzle 62 is disposed above the heat source pipe 61 so that the sprayed mixed dilute solution Sx falls on the heat source pipe 61. In the low temperature regenerator 60, the sprayed mixed dilute solution Sx is heated with the exhausted hot water h, thereby generating a low temperature concentrated solution Sb whose concentration is increased by evaporating the refrigerant V from the mixed dilute solution Sx. The low temperature concentrated solution Sb is configured to be stored in the lower part. A storage part 63 for storing the generated low-temperature concentrated solution Sb is formed in the lower part of the low-temperature regenerator 60. The storage part 63 is divided into a drop storage part 63a and an overflow storage part 63b by a weir 63s, and the low temperature concentrated solution Sb generated by being heated by the exhausted hot water h falls and first falls storage part 63a. The low temperature concentrated solution Sb stored in the fall storage part 63a and exceeding the weir 63s is configured to flow into the overflow storage part 63b.

  The drop storage part 63a of the low temperature regenerator 60 and the low temperature concentrated solution spray nozzle 32 of the low temperature absorber 30 are connected by a low temperature concentrated solution pipe 38 through which the low temperature concentrated solution Sb flows. The low temperature concentrated solution pipe 38 is provided with a low temperature solution pump 66 that pumps the low temperature concentrated solution Sb of the low temperature regenerator 60 to the low temperature absorber 30. The low temperature solution pump 66 has an inverter 66v connected to the low temperature absorber liquid level detector 34 by a signal cable, and the rotation speed is adjusted according to the liquid level detected by the low temperature absorber liquid level detector 34. The flow rate of the low-temperature concentrated solution Sb pumped toward the low-temperature absorber 30 can be adjusted. One end of a mixed dilute solution pipe 37 for flowing the mixed dilute solution Sx is connected to the mixed dilute solution spray nozzle 62, and the high temperature dilute solution pipe 16 and the low temperature dilute solution are connected to the other end of the mixed dilute solution pipe 37. A tube 36 is connected. The low temperature concentrated solution pipe 38 and the low temperature diluted solution pipe 36 are provided with a low temperature solution heat exchanger 68 that performs heat exchange between the low temperature concentrated solution Sb and the low temperature diluted solution Sv.

  In the high temperature regenerator 50, a part of the refrigerant vapor heat source pipe 51 is disposed inside. The refrigerant vapor heat source pipe 51 is not opened in the high temperature regenerator 50, one end is connected to the gas phase part of the high temperature evaporator 20, and the other end is connected to the condenser 70. Then, the refrigerant V in the form of the high-temperature refrigerant vapor Vr is received, changed into the refrigerant liquid Vf by the high-temperature regenerator 50, and then introduced into the condenser 70. The refrigerant vapor heat source pipe 51 is provided with a heat source flow rate adjustment valve 51v as a refrigerant vapor heat source flow rate adjustment valve that adjusts the flow rate of the high temperature refrigerant vapor Vr flowing inside the high temperature regenerator 50 outside. The high temperature regenerator 50 has an intermediate concentrated solution spray nozzle 52 that introduces and sprays the low temperature concentrated solution Sb generated by the low temperature regenerator 60 as an intermediate concentration absorbing liquid. In the present embodiment, the low-temperature concentrated solution Sb (name from the viewpoint of concentration) includes the second absorbent (concentrated solution in the low-temperature absorber 30) and the intermediate-concentrated absorbent (diluted solution in the high-temperature regenerator 50). Also serves as. The intermediate concentrated solution spray nozzle 52 is disposed above the refrigerant vapor heat source pipe 51 so that the sprayed low temperature concentrated solution Sb falls on the refrigerant vapor heat source pipe 51. The intermediate concentrated solution spray nozzle 52 and the overflow storage portion 63b of the low temperature regenerator 60 are connected by an intermediate concentrated solution tube 57 for flowing the low temperature concentrated solution Sb. In the high temperature regenerator 50, the sprayed low temperature concentrated solution Sb is heated by the high temperature refrigerant vapor Vr flowing in the refrigerant vapor heat source pipe 51, whereby the refrigerant V further evaporates from the low temperature concentrated solution Sb and the concentration increases. Concentrated solution Sa is produced | generated and the produced | generated hot concentrated solution Sa is comprised by the lower part.

  The high temperature regenerator 50 is accommodated in the same can body as the low temperature regenerator 60. In the present embodiment, a high-temperature regenerator 50 is disposed at the lower portion of the can body, and a low-temperature regenerator 60 is disposed at the upper portion, and is provided so as to surround the lower side and the side of the heat source pipe 61 therebetween. A partition plate 64 is disposed. The partition plate 64 does not completely separate the high-temperature regenerator 50 and the low-temperature regenerator 60, and both are in communication with each other and are configured to operate at substantially the same pressure (dew point temperature). The portion of the high temperature regenerator 50 in which the high temperature concentrated solution Sa is stored and the high temperature concentrated solution spray nozzle 12 of the high temperature absorber 10 are connected by a high temperature concentrated solution tube 55 through which the high temperature concentrated solution Sa flows. The high temperature concentrated solution tube 55 is provided with a high temperature solution pump 56 that pumps the high temperature concentrated solution Sa of the high temperature regenerator 50 to the high temperature absorber 10. The high temperature solution pump 56 has an inverter 56v connected to the high temperature absorber liquid level detector 14 by a signal cable, and the rotation speed is adjusted according to the liquid level detected by the high temperature absorber liquid level detector 14. The flow rate of the hot concentrated solution Sa that is pumped to the hot absorber 10 and sprayed from the hot concentrated solution spray nozzle 12 can be adjusted. The high temperature concentrated solution tube 55 and the high temperature dilute solution tube 16 (as described above, one end is connected to the storage unit 13 of the high temperature absorber 10 and the other end is connected to the mixed dilute solution tube 37). A high-temperature solution heat exchanger 58 that performs heat exchange between the concentrated solution Sa and the high-temperature dilute solution Sw is provided.

  The condenser 70 has a cooling water pipe 71 that forms a cooling medium flow path. The cooling water c as a cooling medium flows through the cooling water pipe 71. The condenser 70 introduces the regenerator refrigerant vapor Vg in which the vapor of the refrigerant V generated in the high temperature regenerator 50 and the vapor of the refrigerant V generated in the low temperature regenerator 60 are mixed, and cools it with the cooling water c. It is configured to condense. The cooling water pipe 71 is disposed so that the regenerator refrigerant vapor Vg is not immersed in the condensed refrigerant liquid Vf so that the regenerator refrigerant vapor Vg can be directly cooled. The condenser 70 is connected to a refrigerant liquid pipe 75 that sends the condensed refrigerant liquid Vf toward the high temperature evaporator 20 and the low temperature evaporator 40. The refrigerant liquid pipe 75 is connected to the refrigerant liquid pipe 29 connected to the high temperature evaporator 20 and the refrigerant liquid pipe 48 connected to the low temperature evaporator 40, and the refrigerant liquid Vf in the condenser 70 is transferred to the high temperature evaporator 20. And the low-temperature evaporator 40 can be distributed. The refrigerant liquid pipe 75 is provided with a condenser refrigerant pump 76 for pumping the refrigerant liquid Vf. A refrigerant liquid pipe 75 and a refrigerant liquid pipe 45 that guides the refrigerant liquid Vf from the storage portion 43 of the low-temperature evaporator 40 to the condenser 70 are connected to the refrigerant liquid Vf that flows into the condenser 70 and the refrigerant that flows out of the condenser 70. A refrigerant liquid heat exchanger 78 that performs heat exchange with the liquid Vf is disposed.

  The high temperature regenerator 50, the low temperature regenerator 60, and the condenser 70 are formed in one can body so as to communicate with each other. The high temperature regenerator 50, the low temperature regenerator 60, and the condenser 70 communicate with each other, so that the regenerator refrigerant vapor Vg generated in the high temperature regenerator 50 and the low temperature regenerator 60 can be supplied to the condenser 70. Has been. The high temperature regenerator 50, the low temperature regenerator 60, and the condenser 70 communicate with each other in the upper gas phase portion. In the present embodiment, the high temperature regenerator 50, the low temperature regenerator 60, and the condenser 70 are provided below the high temperature absorber 10, the high temperature evaporator 20, the low temperature absorber 30, and the low temperature evaporator 40.

  The gas-liquid separator 80 is a device that introduces the heated medium W that flows through the heating tube 11 of the high-temperature absorber 10 and separates the heated medium vapor Wv and the heated medium liquid Wq. The gas-liquid separator 80 is provided with a gas-liquid separator liquid level detector 81 that detects the liquid level of the heated medium liquid Wq stored inside. The lower part of the gas-liquid separator 80 and one end of the heating pipe 11 of the high-temperature absorber 10 are connected by a heated medium liquid pipe 82 that guides the heated medium liquid Wq to the heating pipe 11. The heated medium liquid pipe 82 is provided with a heated medium pump 83 that pumps the heated medium liquid Wq toward the heated pipe 11. The side surface of the gas-liquid separator 80 whose inside is a gas phase portion and the other end of the heating tube 11 are connected by a heated medium tube 84 after heating that guides the heated medium W to the gas-liquid separator 80. Yes.

  The gas-liquid separator 80 is connected to a makeup water pipe 85 that introduces makeup water Ws for supplementing the heated medium W supplied to the outside of the system as steam from outside the system. The make-up water pipe 85 is supplied with a make-up water pump 86 for pumping make-up water Ws toward the gas-liquid separator 80, a check valve 85c, and a make-up water heat exchanger 87 for preheating the make-up water Ws with warm water. It arrange | positions in this order toward the flow direction of water Ws. The make-up water pump 86 is connected to the gas-liquid separator liquid level detector 81 through a signal cable so that the start / stop is controlled according to the liquid level of the heated medium liquid Wq in the gas-liquid separator 80. It is configured. Further, the heated liquid vapor supply pipe 89 for supplying the heated medium vapor Wv to the outside of the system is connected to the upper part (typically the top) of the gas-liquid separator 80. The heated medium vapor supply pipe 89 is provided with a pressure adjustment valve 89v that adjusts the pressure in the gas-liquid separator 80 by adjusting the flow rate of the heated medium vapor Wv supplied outside the system. The gas-liquid separator 80 is provided with a gas-liquid separator pressure sensor 92 that detects an internal static pressure. The pressure control valve 89v is connected to the gas-liquid separator pressure sensor 92 through a signal cable, and is configured to be able to adjust the opening according to the pressure detected by the gas-liquid separator pressure sensor 92. Yes.

  The gas-liquid separator 80 may introduce a mixed heated medium Wm in which part of the heated medium liquid Wq is evaporated in the heating tube 11 and the heated medium liquid Wq and the heated medium vapor Wv are mixed. Alternatively, the heated medium liquid Wq may be guided to the gas-liquid separator 80, and the pressure may be reduced to partially vaporize the mixed heated medium Wm for gas-liquid separation. In order to vaporize the medium to be heated Wq under reduced pressure, a throttle means such as an orifice can be used. Whether or not a part of the heated medium liquid Wq is evaporated in the heating pipe 11 is typically determined by adjusting the discharge pressure of the heated medium pump 83 and / or the make-up water pump 86. The internal pressure can be adjusted by whether or not the internal pressure is higher than a saturation pressure corresponding to the temperature of the heated medium liquid Wq.

  The control device 99 is a device that controls the operation of the absorption heat pump 1. The control device 99 is connected to the condenser refrigerant pump 76 and the heated medium pump 83 via signal cables, respectively, and is configured to be able to start / stop and adjust the rotation speed. In the description so far, the output of the high-temperature absorber liquid level detector 14 is directly input and controlled, and the output of the high-temperature solution pump 56 and the low-temperature absorber liquid level detector 34 is directly input and controlled. The replenishing water pump 86 that is controlled by directly inputting the output of the low-temperature solution pump 66 and the gas-liquid separator liquid level detector 81 are also connected via the control device 99 (the output signal of the detector is temporarily set). It is good also as being controlled by inputting into the control apparatus 99. FIG. The control device 99 is connected to the heat source flow rate adjustment valve 51v by a signal cable, and is configured to be able to adjust the opening degree of the heat source flow rate adjustment valve 51v. In the description so far, the output of the high-temperature evaporator liquid level detector 26 is directly input and controlled. The two-way valve 29v and the output of the low-temperature evaporator liquid level detector 44 are directly input and controlled. The flow rate control valve 48v and the pressure control valve 89v that are controlled by directly inputting the output of the gas-liquid separator pressure sensor 92 are also connected via the control device 99 (the output signal of the detector is once controlled by the control device). It is also possible to be controlled (by inputting to 99).

  With continued reference to FIG. 1, the operation of the absorption heat pump 1 will be described. First, the refrigerant side cycle will be described. In the condenser 70, the regenerator refrigerant vapor Vg generated in the high temperature regenerator 50 and the low temperature regenerator 60 is received, cooled and condensed with the cooling water c flowing through the cooling water pipe 71, and the refrigerant liquid Vf is obtained. The condensed refrigerant liquid Vf is pumped by the condenser refrigerant pump 76 toward the high temperature evaporator 20 and the low temperature evaporator 40. The refrigerant liquid Vf pumped by the condenser refrigerant pump 76 flows through the refrigerant liquid pipe 75, and then is divided into the refrigerant liquid pipe 29 and the refrigerant liquid pipe 48. The refrigerant liquid Vf flowing through the refrigerant liquid pipe 29 is the refrigerant gas-liquid. The refrigerant liquid Vf introduced into the separation cylinder 21 and flowing through the refrigerant liquid pipe 48 is sprayed from the refrigerant liquid spray nozzle 42. At this time, the two-way valve according to the detected liquid level of the high-temperature evaporator liquid level detector 26 so that the refrigerant liquid Vf accumulated in the lower part of the refrigerant gas-liquid separation cylinder 21 of the high-temperature evaporator 20 becomes a predetermined liquid level. 29v is controlled, and the flow rate adjustment valve 48v is controlled according to the detected liquid level of the low temperature evaporator liquid level detector 44 so that the refrigerant liquid Vf in the storage unit 43 of the low temperature evaporator 40 becomes a predetermined liquid level. The

  The refrigerant liquid Vf sprayed from the refrigerant liquid spray nozzle 42 is heated and evaporated by the exhausted hot water h flowing in the heat source pipe 41 to become a low-temperature refrigerant vapor Vs. The low-temperature refrigerant vapor Vs generated in the low-temperature evaporator 40 moves to the low-temperature absorber 30 that communicates with the low-temperature evaporator 40. On the other hand, the refrigerant liquid Vf introduced into the refrigerant gas-liquid separation cylinder 21 is sent to the heating pipe 31 of the low-temperature absorber 30 by gravity. The refrigerant liquid Vf sent to the heating pipe 31 is generated in the low temperature absorber 30 when the low temperature refrigerant vapor Vs generated in the low temperature evaporator 40 and moved to the low temperature absorber 30 is absorbed by the low temperature concentrated solution Sb. It is heated by the absorbed heat, and evaporates by this heating to become high-temperature refrigerant vapor Vr. Since the high-temperature refrigerant vapor Vr generated in the heating pipe 31 has a lower density than the refrigerant liquid Vf, the high-temperature refrigerant vapor Vr rises toward the high-temperature evaporator 20 and flows through the high-temperature refrigerant vapor receiving pipe 24 to reach the refrigerant gas-liquid separation cylinder 21. Then, it moves to the high-temperature absorber 10 that communicates with the high-temperature evaporator 20. Further, part of the high-temperature refrigerant vapor Vr that has reached the refrigerant gas-liquid separation cylinder 21 enters the refrigerant vapor heat source pipe 51, and in the high-temperature regenerator 50, the low-temperature concentrated solution Sb sprayed from the intermediate concentrated solution spray nozzle 52. The condensed refrigerant liquid Vf is deprived of heat and flows into the condenser 70. Thus, the high-temperature refrigerant vapor Vr in the refrigerant vapor heat source pipe 51 flows toward the condenser 70 without requiring special power.

  Next, the cycle on the absorption liquid side of the absorption heat pump 1 will be described. In the high-temperature absorber 10, the hot concentrated solution Sa is sprayed from the hot concentrated solution spray nozzle 12, and the sprayed hot concentrated solution Sa absorbs the high-temperature refrigerant vapor Vr that has moved from the high-temperature evaporator 20. The high temperature concentrated solution Sa that has absorbed the high temperature refrigerant vapor Vr is reduced in concentration to become a high temperature diluted solution Sw. In the high-temperature absorber 10, heat of absorption is generated when the high-temperature concentrated solution Sa absorbs the high-temperature refrigerant vapor Vr. The absorbed medium liquid Wq flowing through the heating tube 11 is heated by the absorbed heat. Here, the operation around the gas-liquid separator 80 for taking out the heated medium vapor Wv will be described.

  The gas-liquid separator 80 is introduced with makeup water Ws from outside the system via a makeup water pipe 85. The makeup water Ws is pumped through the makeup water pipe 85 by the makeup water pump 86 and is introduced into the gas-liquid separator 80 after the temperature rises by the makeup water heat exchanger 87. The makeup water Ws introduced into the gas-liquid separator 80 is stored in the lower part of the gas-liquid separator 80 as the heated medium liquid Wq. The makeup water pump 86 is controlled so that the heated medium liquid Wq stored in the lower part of the gas-liquid separator 80 becomes a predetermined liquid level. The heated medium liquid Wq stored in the lower part of the gas-liquid separator 80 is sent to the heating tube 11 of the high-temperature absorber 10 by the heated medium pump 83. The heated medium liquid Wq sent to the heating tube 11 is heated by the above-described absorption heat in the high-temperature absorber 10. The heated medium liquid Wq heated by the heating tube 11 is gas-liquid separated as a mixed heated medium Wm partially evaporated to become a heated medium vapor Wv, or as a heated medium liquid Wq whose temperature has increased. Flows through the heated medium tube 84 after heating toward the vessel 80. When the heated medium liquid Wq whose temperature has risen flows through the heated medium pipe 84 after heating, the heated medium liquid Wq is depressurized when being introduced into the gas-liquid separator 80, and a part of the heated medium liquid Wq is evaporated and covered. The mixed medium to be heated Wm that has become the heating medium vapor Wv is introduced into the gas-liquid separator 80. In the mixed heated medium Wm introduced into the gas-liquid separator 80, the heated medium liquid Wq and the heated medium vapor Wv are separated. The separated heated medium liquid Wq is stored in the lower part of the gas-liquid separator 80 and sent again to the heating tube 11 of the high-temperature absorber 10. On the other hand, the separated heated medium vapor Wv is led out to the heated medium vapor supply pipe 89 and supplied to the vapor use place. In the present embodiment, the heated medium vapor Wv exceeding 0.2 to 0.4 MPa (gauge pressure) is led out from the gas-liquid separator 80, and the temperature of the exhaust hot water h is raised to 0.8 MPa ( The heated medium vapor Wv having a pressure of about the gauge pressure) or an arbitrary pressure therebetween is derived.

  Returning to the description of the cycle on the absorption liquid side of the absorption heat pump 1 again. The high-temperature concentrated solution Sa that has absorbed the high-temperature refrigerant vapor Vr by the high-temperature absorber 10 is reduced in concentration to become a high-temperature dilute solution Sw, and is stored in the storage unit 13. The high-temperature dilute solution Sw in the reservoir 13 flows through the high-temperature dilute solution tube 16 toward the low-temperature regenerator 60 due to the difference between gravity and internal pressure, and heat exchanges with the high-temperature concentrated solution Sa in the high-temperature solution heat exchanger 58 so that the temperature is increased. After being lowered, it flows into the mixed dilute solution tube 37. On the other hand, in the low-temperature absorber 30, the low-temperature concentrated solution Sb is sprayed from the low-temperature concentrated solution spray nozzle 32 toward the heating pipe 31, absorbs the low-temperature refrigerant vapor Vs that has moved from the low-temperature evaporator 40, and is generated at that time. The refrigerant liquid Vf flowing in the heating pipe 31 is heated by the absorbed heat to be converted into a high-temperature refrigerant vapor Vr. The low-temperature concentrated solution Sb that has absorbed the low-temperature refrigerant vapor Vs decreases in concentration to become a low-temperature dilute solution Sv and is stored in the storage unit 33. The low-temperature dilute solution Sv in the storage unit 33 is sent toward the low-temperature regenerator 60 due to the difference between gravity and internal pressure. When the low-temperature dilute solution Sv flows through the low-temperature dilute solution tube 36 from the low-temperature absorber 30 toward the low-temperature regenerator 60, the low-temperature dilute solution Sv exchanges heat with the low-temperature concentrated solution Sb derived from the drop storage unit 63a by the low-temperature solution heat exchanger 68. After the temperature drops, the mixed dilute solution pipe 37 flows. The low temperature dilute solution Sv that has flowed into the mixed dilute solution tube 37 is mixed with the high temperature dilute solution Sw that has also flowed into the mixed dilute solution tube 37 to form a mixed dilute solution Sx, which is sent to the low temperature regenerator 60. The mixed dilute solution Sx sent to the low temperature regenerator 60 is sprayed from the mixed dilute solution spray nozzle 62. The mixed dilute solution Sx sprayed from the mixed dilute solution spray nozzle 62 is heated by the exhaust hot water h (about 80 ° C. in this embodiment) flowing through the heat source pipe 61, and the refrigerant V in the sprayed mixed dilute solution Sx. A part of the water vapor evaporates and the concentration rises to become a low-temperature concentrated solution Sb, which is first stored in the drop reservoir 63a of the low-temperature regenerator 60, and the liquid level in the drop reservoir 63a rises and exceeds the weir 63s. It is stored in the flow storage unit 63b.

  The low temperature concentrated solution Sb stored in the drop storage unit 63a of the low temperature regenerator 60 is pumped by the low temperature solution pump 66 to the low temperature concentrated solution spray nozzle 32 of the low temperature absorber 30 via the low temperature concentrated solution pipe 38. At this time, the inverter 66v according to the detected liquid level of the low temperature absorber liquid level detector 34 so that the liquid level of the low temperature diluted solution Sv stored in the storage unit 33 of the low temperature absorber 30 becomes a predetermined liquid level. The rotational speed (and hence the discharge flow rate) of the low temperature solution pump 66 is adjusted. The low-temperature concentrated solution Sb flowing through the low-temperature concentrated solution pipe 38 heat-exchanges with the low-temperature dilute solution Sv in the low-temperature solution heat exchanger 68 and rises in temperature, and then flows into the low-temperature absorber 30. Be sprayed. On the other hand, the low temperature concentrated solution Sb stored in the overflow storage unit 63 b is introduced into the high temperature regenerator 50 through the intermediate concentrated solution pipe 57 and sprayed from the intermediate concentrated solution spray nozzle 52. The low-temperature concentrated solution Sb sprayed from the intermediate concentrated solution spray nozzle 52 is heated and concentrated by the high-temperature refrigerant vapor Vr flowing in the refrigerant vapor heat source pipe 51, and a part of the refrigerant V evaporates to increase the concentration. The solution Sa is stored in the lower part of the high temperature regenerator 50. On the other hand, the refrigerant V evaporated from the low temperature concentrated solution Sb merges with the vapor of the refrigerant V generated in the low temperature regenerator 60 and moves to the condenser 70 as the regenerator refrigerant vapor Vg. The high temperature concentrated solution Sa stored in the lower part of the high temperature regenerator 50 is pumped by the high temperature solution pump 56 toward the high temperature concentrated solution spray nozzle 12 of the absorber 10 via the high temperature concentrated solution tube 55, and high temperature solution heat exchange is performed. After the temperature rises due to heat exchange with the hot dilute solution Sw in the vessel 58, the hot melt solution spray nozzle 12 is reached. At this time, the high temperature solution pump is driven by the inverter 56v according to the detected liquid level of the high temperature absorber liquid level detector 14 so that the high temperature dilute solution Sw stored in the storage unit 13 of the high temperature absorber 10 becomes a predetermined liquid level. The rotational speed 56 (and thus the discharge flow rate) is adjusted. The hot concentrated solution Sa that has reached the hot concentrated solution spray nozzle 12 is sprayed from the hot concentrated solution spray nozzle 12, and thereafter the same cycle is repeated.

  The explanation of the operation of the absorption heat pump 1 will be supplemented also with reference to the Dueling diagram of FIG. In the Dueling diagram of FIG. 2, the vertical axis represents the dew point temperature of the refrigerant V (water in the present embodiment), and the horizontal axis represents the temperature of the absorbing liquid S (LiBr aqueous solution in the present embodiment). The line rising to the right represents the isoconcentration line of the absorbent S, and the concentration increases toward the right and decreases toward the left. The line rising toward the right passing through the origin in the figure has a solution concentration of 0% (that is, only the refrigerant). It is a line. Since the dew point temperature indicated by the vertical axis has a corresponding relationship with the saturation pressure, in the heat pump cycle of the present embodiment in which the refrigerant vapors Vr, Vs, and Vg are saturated vapors, the vertical axis indicates the main constituent members 10, 20, 30. , 40, 50, 60, 70 can be viewed as representing the internal pressure.

  In FIG. 2, the state of the absorbing liquid S in the rated operation of the absorption heat pump 1 is represented by a solution line SD, and the state of the refrigerant V in the rated operation is represented by a refrigerant line VD. In FIG. 2, states P12, P13, P32, and P33 represent the states of the absorbing liquid S in the high temperature concentrated solution spray nozzle 12, the storage unit 13, the low temperature concentrated solution spray nozzle 32, and the storage unit 33, respectively. P63 and P53 represent the states of the absorbing liquid S in the mixed dilute solution spray nozzle 62, the storage unit 63, and the intermediate concentrated solution spray nozzle 52, respectively. The fact that the states P12 to P13, the states P32 to P33, and the states P62 to P63 to P52 extend in the horizontal direction indicates that the concentration of the absorbing liquid S changes under the same pressure. Further, the state P20 represents the state of the high temperature evaporator 20, the state P40 represents the state of the low temperature evaporator 40, and the state P70 represents the state of the condenser 70. As apparent from FIG. 2, in this embodiment, the pressures of the high temperature absorber 10 and the high temperature evaporator 20, the low temperature absorber 30 and the low temperature evaporator 40, the high temperature regenerator 50, the low temperature regenerator 60 and the condenser 70 are as follows. Are equal. Note that the high-temperature absorber 10 and the high-temperature evaporator 20, the low-temperature absorber 30 and the low-temperature evaporator 40, the high-temperature regenerator 50, the low-temperature regenerator 60, and the condenser 70 that are in communication with each other to move the vapor of the refrigerant V. Strictly speaking, the internal pressure is lower on the downstream side of the vapor of the refrigerant V by a pressure loss due to the flow of the vapor of the refrigerant V, but is almost the same pressure.

  The absorbing liquid S circulates counterclockwise on the solution line SD. As shown in states P62 to P63, in the low temperature regenerator 60, the temperature of the absorbing liquid S rises as it receives the waste heat Hh from the waste water h, and the concentration rises, and the mixed dilute solution Sx becomes the low temperature concentrated solution Sb. . The refrigerant V generated in the low temperature regenerator 60 with the increase in the concentration of the absorbent S flows into the condenser 70 as the regenerator refrigerant vapor Vg together with the refrigerant V generated in the high temperature regenerator 50 and is cooled. (State P70). The refrigerant V of the low-temperature evaporator 40 in the state P40 receives the exhaust heat from the exhaust hot water h to become the low-temperature refrigerant vapor Vs, which is absorbed by the low-temperature concentrated solution Sb of the low-temperature absorber 30 and shown in the states P32 to P33. As such, the concentration of the low temperature concentrated solution Sb is lowered. Absorption heat H20 generated by the low-temperature concentrated solution Sb absorbing the low-temperature refrigerant vapor Vs in the states P32 to P33 heats the refrigerant V of the high-temperature evaporator 20 in the state P20, and makes this the high-temperature refrigerant vapor Vr. Then, the high-temperature refrigerant vapor Vr generated by the absorption heat H20 is absorbed by the high-temperature concentrated solution Sa of the high-temperature absorber 10 to reduce the concentration of the high-temperature concentrated solution Sa as shown in the states P12 to P13. The absorption heat Hw generated by the high temperature concentrated solution Sa in the states P12 to P13 absorbing the high temperature refrigerant vapor Vr heats the medium W to be heated. Thereby, it becomes possible to raise the temperature of the to-be-heated medium W to the temperature vicinity of the hot dilute solution Sw in the state P13. If the boiling point of the heated medium liquid Wq exceeds the boiling point in the process of increasing the temperature of the heated medium W, the heated medium vapor Wv can be generated.

  In the high temperature regenerator 50 corresponding to the lower part of the solution line SD, as shown in the states P63 to P53, the temperature of the absorbing liquid S rises as a result of receiving the retained heat H50 of the high temperature refrigerant vapor Vr, and the concentration increases. The solution Sb becomes the hot concentrated solution Sa. In FIG. 2, the slope of the diagram indicating the movement of the retained heat H50 of the high-temperature refrigerant vapor Vr is large and the temperature change seems to be small, but the high-temperature refrigerant vapor Vr is heated when the absorbing liquid S is heated in the states P63 to P53. The state is changed from the gas phase to the liquid phase, that is, latent heat is given to the absorbing liquid S of the high temperature regenerator 50. Therefore, the retained heat H50 given to the absorbing liquid S of the high-temperature regenerator 50 becomes an extremely large amount of heat as compared with the case where sensible heat accompanying temperature change is given, and the low-temperature concentrated solution Sb is effectively regenerated into the high-temperature concentrated solution Sa. be able to. Further, since the exhaust heat Hh is used when the absorbing liquid S in the states P62 to 63 is concentrated, the use of the retained heat H50 of the high-temperature refrigerant vapor Vr can be reduced by making maximum use of the exhaust heat Hh. And COP can be improved. Since the amount of retained heat H50 given to the absorbent S of the high-temperature regenerator 50 can be adjusted by adjusting the opening of the heat source flow rate adjustment valve 51v, the heat source flow rate adjustment valve 51v is a heat amount adjustment means. It is one form.

  FIG. 3 shows a Duhring diagram of a three-stage temperature rising type absorption heat pump according to a reference example. (A) is a series flow of the absorbent, and (b) is a parallel flow of the absorbent. In FIG. 3A, the combination of the absorber and the evaporator is provided in three stages. The absorption heat in the low temperature absorber AL is used to evaporate the refrigerant of the intermediate temperature evaporator EM, and the intermediate temperature absorption is performed. The absorption heat in the evaporator AM is used to evaporate the refrigerant in the high temperature evaporator EH. The high temperature absorber AH is condensed to the same pressure as the high temperature evaporator EH, and the low temperature evaporator EL is condensed to the same pressure as the low temperature absorber AL. The vessel C and the regenerator G are at the same pressure. In FIG. 3B, the combination of the absorber and the regenerator is provided in three stages. The absorption heat in the low temperature absorber AL is used to regenerate the absorption liquid in the intermediate temperature regenerator GM. Absorption heat in the absorber AM is used to regenerate the absorption liquid of the high temperature regenerator GH. The high temperature absorber AH and the evaporator E have the same pressure as the low temperature absorber AL and intermediate temperature absorber AM, and the low temperature regenerator GL. The condenser C has the same pressure as the high temperature regenerator GH and the medium temperature regenerator GM.

  Looking again at the During diagram (see FIG. 2) of the absorption heat pump 1 according to the present embodiment, the solution line SD indicating the cycle of the absorption liquid S has two stages in the concentration direction and two stages in the pressure direction. It shows a three-stage cycle that combines the cycle. By being comprised in this way, the temperature increase range which produces | generates the to-be-heated medium vapor | steam Wv from the exhausted hot water h introduce | transduced can be enlarged. When the absorption heat pump 1 according to the present embodiment is compared with the three-stage temperature rising absorption heat pump according to the reference example in the Duering diagram, the maximum pressure is lower than that shown in FIG. It has become. In this way, the absorption heat pump 1 can suppress an increase in internal pressure, relax the conditions from the viewpoint of the strength of the can body, and suppress the necessary head of the pump for circulating the absorbing liquid S and the refrigerant V. As a result, the increase in power can be prevented. Further, the absorption heat pump 1 has a lower maximum concentration of the absorbing liquid S than that shown in FIG. Thus, the absorption heat pump 1 can suppress an excessive increase in the concentration of the absorption liquid S, and a stable operation that avoids crystals of the absorption liquid S is possible. As described above, the absorption heat pump 1 according to the present embodiment uses the heat input to the low-temperature regenerator 60 to the maximum extent, so that the COP can be improved while improving the temperature raising capability. Can be improved.

  Next, with reference to FIG. 4, the absorption heat pump 2 which concerns on the 2nd Embodiment of this invention is demonstrated. 4A and 4B are diagrams for explaining the absorption heat pump 2, wherein FIG. 4A is a schematic system diagram, and FIG. 4B is a Duling diagram. The absorption heat pump 2 is a three-stage temperature rising type absorption heat pump. In the absorption heat pump 2, as compared with the absorption heat pump 1 (see FIG. 1), the high-temperature dilute solution pipe 16 is connected to the solution spray nozzle 32A in the low-temperature absorber 30 (not the mixed dilute solution pipe 37 (see FIG. 1)). The low temperature dilute solution pipe 36 is connected to the solution spray nozzle 62A in the low temperature regenerator 60 (not the mixed dilute solution pipe 37 (see FIG. 1)), the low temperature solution heat exchanger 68 (see FIG. In place of the high-temperature solution heat exchanger 58, and exchanges heat between the high-temperature concentrated solution Sa and the low-temperature dilute solution Sv. The solution heat exchanger 68A to be performed is provided, the storage unit 63 of the low temperature regenerator 60 is not divided, and the low temperature concentrated solution pipe 38 (see FIG. 1) and the low temperature solution pump 66 (see FIG. 1) are provided. Low temperature concentrated solution Sb in the reservoir 63 With all the points guided to the high temperature regenerator 50 and the above configuration, the absorbent S flows in the order of the high temperature absorber 10, the low temperature absorber 30, the low temperature regenerator 60, and the high temperature regenerator 50 and returns to the high temperature absorber 10 again. The difference is that it is structured in series flow. With this configuration, in the absorption heat pump 2, the high-temperature dilute solution Sw is the second absorption liquid. Further, the absorption heat pump 2 has a configuration of absorption heat transfer means for transferring the heat generated by the low temperature absorber 30 to the high temperature regenerator 50 as compared with the absorption heat pump 1 (see FIG. 1). In place of the refrigerant vapor heat source pipe 51 (see FIG. 1) that is transported in the form of the above, a circulating heat medium pipe of a closed pipe that circulates the liquid heat medium t between the low temperature absorber 30 and the high temperature regenerator 50 251 is provided, and the circulating heat medium pipe 251 is provided with a circulating heat medium pump 259 for circulating the heat medium t. The circulating heat medium pipe 251 is arranged in the form of replacing the refrigerant vapor heat source pipe 51 (see FIG. 1) in the high temperature regenerator 50, but is provided side by side with the heating pipe 31 in the low temperature absorber 30. The configuration other than the above is the same as that of the absorption heat pump 1 (see FIG. 1).

  In the absorption heat pump 2 configured as described above, the absorbing liquid S circulates counterclockwise on the solution line SD2 in the Duering diagram shown in FIG. As shown in states P12 to P13, the hot dilute solution Sw whose concentration has decreased from the hot concentrated solution Sa in the high temperature absorber 10 absorbs the low temperature refrigerant vapor Vs in the low temperature absorber 30, and further as shown in states P32A to P33. The concentration is lowered to a low temperature dilute solution Sv. When the hot dilute solution Sw in the states P32A to P33 absorbs the low-temperature refrigerant vapor Vs, absorption heat H20 and H502 are generated, and the absorption heat H20 heats the refrigerant V of the high-temperature evaporator 20 in the state P20 to heat the high-temperature refrigerant. The absorbed heat H502 is transferred to the high-temperature regenerator 50 by heating the heat medium t in the circulating heat medium pipe 251 as steam Vr. The low-temperature dilute solution Sv is then introduced into the low-temperature regenerator 60 and receives the exhaust heat Hh from the exhaust hot water h as shown in the states P62A to P63. Sb. Thereafter, as shown in states P63 to P53, the low temperature concentrated solution Sb introduced into the high temperature regenerator 50 is heated and concentrated by the heat medium t flowing in the circulating heat medium pipe 251 to become a high temperature concentrated solution Sa, and again the high temperature absorber. 10 is conveyed. The heat transferred from the low temperature absorber 30 to the high temperature regenerator 50 via the heat medium t can be adjusted by changing the discharge flow rate of the circulation heat medium pump 259. It is one form of an adjustment means. As described above, in the absorption heat pump 2, the absorption liquid S is first heated by the low temperature regenerator 60 in the process of regenerating from the low temperature dilute solution Sv to the high temperature concentrated solution Sa by the low temperature regenerator 60 and the high temperature regenerator 50. The exhaust heat Hh is used when being concentrated, and then the absorption heat H502 in the low-temperature absorber 30 is used when the absorption liquid S is heated and concentrated in the high-temperature regenerator 50, so that the exhaust heat Hh is maximized. Therefore, the COP can be improved.

  In the above description of the absorption heat pump 2, the absorption heat transfer means circulates the liquid heat medium t 251 between the low temperature absorber 30 and the high temperature regenerator 50, and the circulation heat medium pipe 251. Although it has decided to have the circulation heat medium pump 259 which circulates the heat medium t, the refrigerant which conveys the heat absorbed in the low-temperature absorber 30 once in the form of the high-temperature refrigerant vapor Vr, like the absorption heat pump 1. It is good also as having the steam heat source pipe | tube 51. FIG. On the contrary, the absorption heat pump 1 of the absorption heat pump 1, like the absorption heat pump 2, circulates the heat medium tube 251 that circulates the liquid heat medium t between the low temperature absorber 30 and the high temperature regenerator 50, and the circulation heat. A circulation heat medium pump 259 that circulates the heat medium t in the medium pipe 251 may be included. That is, between the absorption heat pump 1 (see FIG. 1) and the absorption heat pump 2 (see FIG. 4), the configuration of the flow of the absorbing liquid S and the absorption heat transfer means may be interchanged.

  Further, as shown in the partial system diagram around the low-temperature absorber 30 in FIG. 5, the low-temperature concentrated solution pipe 38 in the absorption heat pump 1 (see FIG. 1) or the high-temperature diluted solution pipe 16 in the absorption heat pump 2 (see FIG. 4) A bypass pipe 35 is provided for bypassing the spray nozzles 32 and 32A to the absorption liquid S flowing in the interior and leading to the storage section 33, and a flow rate adjustment valve 35v whose opening degree can be adjusted by a signal from the control device 99 in the bypass pipe 35. And the spraying flow rate of the absorbing liquid S that absorbs the low-temperature refrigerant vapor Vs in the low-temperature absorber 30 can be adjusted. In this case, the bypass pipe 35 and the flow rate adjusting valve 35v constitute an absorbent liquid flow rate adjusting means. With this configuration, the amount of heat absorbed by the low-temperature absorber 30 can be adjusted, and consequently the amount of absorbed heat H50 and H502 input to the high-temperature regenerator 50 can be adjusted. Thereby, it is possible to avoid the crystal of the absorbing liquid S in the high temperature regenerator 50.

  In the above description, all of the high temperature dilute solution Sw of the high temperature absorber 10 is introduced directly or indirectly into the low temperature regenerator 60. However, a part of the high temperature dilute solution Sw is introduced into the low temperature regenerator 60. However, the remainder of the high-temperature dilute solution Sw may be partially heated by the low-temperature regenerator 60 by skipping (removing) the low-temperature regenerator 60 and introducing it into the high-temperature regenerator 50. In other words, in this configuration, the cycle of the absorbing liquid S is configured separately in the system of the high-temperature absorber 10 and the high-temperature regenerator 50 and the system of the low-temperature absorber 30 and the low-temperature regenerator 60. A part of the heating and concentration of the absorbent S in the system of the absorber 10 and the high-temperature regenerator 50 is performed in the low-temperature regenerator 60, and the COP is reduced by reducing the heating and concentration of the absorbent S in the high-temperature regenerator 50. Can be improved.

  In the above description, the high temperature regenerator 50 and the low temperature regenerator 60 are accommodated in the same can body, and the high temperature regenerator 50 is disposed in the lower portion of the can body, and the low temperature regenerator 60 is disposed in the upper portion. However, the high temperature regenerator 50 may be disposed at the top and the low temperature regenerator 60 may be disposed at the bottom, and the high temperature regenerator 50 and the low temperature regenerator 60 may be disposed side by side. (In the case of such a configuration, a pump for conveying the absorbing liquid S from the low temperature regenerator 60 to the high temperature regenerator 50 is typically provided.) Further, the vapor of the refrigerant V evaporated in the high temperature regenerator 50 and the vapor of the refrigerant V evaporated in the low temperature regenerator 60 are condensed in the common condenser 70, but the refrigerant V evaporated in the high temperature regenerator 50 is used. You may provide separately the condenser which condenses this vapor | steam, and the condenser which condenses the vapor | steam of the refrigerant | coolant V evaporated by the low temperature regenerator 60 separately. In this case, the high-temperature regenerator 50 and the condenser for the high-temperature regenerator 50 are combined with the condenser for the low-temperature regenerator 60 and the low-temperature regenerator 60 so that they are accommodated in different can bodies. Is preferred.

  In the above description, the vapor of the refrigerant V generated in the high temperature regenerator 50 is guided to the condenser 70 without particularly exchanging heat with other fluids. However, it passes through the periphery of the heat source pipe 61 of the low temperature regenerator 60. Thus, the low-temperature dilute solution Sv sprayed from the low-temperature dilute solution spray nozzle 62 may be heated and then guided to the condenser 70. In this way, the energy of the vapor of the high-temperature refrigerant V generated in the high-temperature regenerator 50 can be given to the low-temperature dilute solution Sv heated and concentrated in the low-temperature regenerator 60, and the external heat source ( The required amount of the waste water h) can be reduced, leading to an improvement in COP.

1, 2 Absorption heat pump 11 Heating pipe 10 High temperature absorber 20 High temperature evaporator 30 Low temperature absorber 35 Bypass pipe 35v Flow rate control valve 40 Low temperature evaporator 50 High temperature regenerator 51 Refrigerant vapor heat source pipe 51v Heat source flow rate control valve 60 Low temperature regenerator 70 Condenser 251 Circulating heat medium pipe 259 Circulating heat medium pump Sa High temperature concentrated solution Sb Low temperature concentrated solution Sv Low temperature diluted solution Sw High temperature diluted solution Sx Mixed diluted solution Vf Refrigerant liquid Vg Regenerator refrigerant vapor Vr High temperature refrigerant vapor Vs Low temperature refrigerant vapor W Heating medium t Heating medium

Claims (4)

A first absorber that has a flow path for the medium to be heated, and that heats the medium to be heated with absorption heat generated when the first absorption liquid absorbs the first refrigerant vapor;
An evaporator for supplying the first refrigerant vapor to the first absorber;
More than the first absorber, wherein the first refrigerant vapor is generated by heating the refrigerant liquid in the evaporator with absorption heat generated when the second absorption liquid absorbs the second refrigerant vapor. A second absorber with a low operating temperature;
The first absorbent absorbs the first refrigerant vapor in the first absorber and introduces a dilute solution having a reduced concentration directly or indirectly, and the second absorber introduces the first solution. The second absorption liquid absorbs the second refrigerant vapor and introduces a diluted solution having a reduced concentration, and heats to evaporate the refrigerant from the diluted solution to generate an intermediate concentration absorption liquid having an increased concentration. 1 regenerator;
A second regenerator that introduces the intermediate concentration absorbing liquid from the first regenerator and heats it to produce the first absorbing liquid, and has a lower operating pressure than the evaporator ;
E Bei the absorption heat transfer means for transferring the heat of absorption generated at the second absorber, directly or indirectly to the second regenerator;
The absorption heat transfer means is a refrigerant vapor heat source pipe that allows the first refrigerant vapor in the evaporator to flow inside without requiring special power, and is arranged to pass through the second regenerator. Composed of installed refrigerant vapor heat source pipes;
Absorption heat pump. A refrigerant vapor heat source flow rate adjustment valve for adjusting a flow rate of the first refrigerant vapor flowing in the refrigerant vapor heat source pipe;
The absorption heat pump according to claim 1. Regenerator refrigerant vapor in which refrigerant evaporated from the dilute solution in the first regenerator and refrigerant evaporated from the intermediate concentration absorption liquid in the second regenerator is introduced and cooled to condense into a refrigerant liquid Equipped with a vessel;
The first regenerator, the second regenerator, and the condenser are formed in one can body so as to communicate with each other;
The absorption heat pump according to claim 1 or 2 . An absorption liquid flow rate adjusting means for adjusting a flow rate of the second absorption liquid that absorbs the second refrigerant vapor among the second absorption liquid introduced into the second absorber;
The absorption heat pump according to any one of claims 1 to 3.

Images